US9320985B2 - Configurations and methods of generating low-pressure steam - Google Patents

Configurations and methods of generating low-pressure steam Download PDF

Info

Publication number
US9320985B2
US9320985B2 US13/390,024 US200913390024A US9320985B2 US 9320985 B2 US9320985 B2 US 9320985B2 US 200913390024 A US200913390024 A US 200913390024A US 9320985 B2 US9320985 B2 US 9320985B2
Authority
US
United States
Prior art keywords
steam
consuming device
pressure
generator
condensate
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Active, expires
Application number
US13/390,024
Other languages
English (en)
Other versions
US20120204817A1 (en
Inventor
Jeffrey Scherffius
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Fluor Technologies Corp
Original Assignee
Fluor Technologies Corp
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Fluor Technologies Corp filed Critical Fluor Technologies Corp
Assigned to FLUOR TECHNOLOGIES CORPORATION reassignment FLUOR TECHNOLOGIES CORPORATION ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: SHERFFIUS, JEFFREY
Assigned to FLUOR TECHNOLOGIES CORPORATION reassignment FLUOR TECHNOLOGIES CORPORATION ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: SCHERFFIUS, JEFFREY
Publication of US20120204817A1 publication Critical patent/US20120204817A1/en
Application granted granted Critical
Publication of US9320985B2 publication Critical patent/US9320985B2/en
Active legal-status Critical Current
Adjusted expiration legal-status Critical

Links

Images

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/14—Fractional distillation or use of a fractionation or rectification column
    • B01D3/32—Other features of fractionating columns ; Constructional details of fractionating columns not provided for in groups B01D3/16 - B01D3/30
    • B01D3/322—Reboiler specifications
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K25/00—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for
    • F01K25/04—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for the fluid being in different phases, e.g. foamed
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
    • Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working
    • Y02P70/34—
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P80/00—Climate change mitigation technologies for sector-wide applications
    • Y02P80/10—Efficient use of energy, e.g. using compressed air or pressurized fluid as energy carrier
    • Y02P80/15—On-site combined power, heat or cool generation or distribution, e.g. combined heat and power [CHP] supply

Definitions

  • the field of the invention is devices and methods of low-pressure steam generation at steam consumption pressure for steam consuming devices.
  • Steam is used is numerous plants and methods to provide utility heating to reboilers and other devices.
  • steam heaters are commonly used in the stripper reboiler of an amine plant (e.g., those using the ECONAMINE FG PLUS SM (Fluor Technologies Corp.) process) for regeneration of a solvent for CO 2 capture.
  • the required steam pressure in the reboiler is typically determined by the specific reboiler configuration and process demand
  • the available steam pressure in most plants is often dictated by an external utility system and is invariably higher than the pressure required by the reboiler, as in most known systems steam is generated at fixed pressure intervals. Consequently, heat recovery in the steam generation process is less than desirable.
  • steam generation in external utility systems often precludes waste heat recovery from various sources.
  • the present invention is directed to devices and methods of steam generation for one or more steam consuming devices where the steam is generated by and delivered from the steam generator at about the same pressure at which the steam condenses in the steam consuming device.
  • the steam is generated at the consumption pressure, more heat can be recovered from the heat source(s) used in the steam generation.
  • a plant in one aspect of the inventive subject matter, includes a steam generator that is coupled to a steam consuming device, wherein the steam generator produces steam at a pressure that is substantially equal to the condensing pressure of the steam in the steam consuming device. At least one heat source is thermally coupled to the steam generator to provide heat sufficient for converting the steam condensate from the steam consuming device into steam.
  • a vessel is coupled to the steam generator and the steam consuming device such that the vessel receives the steam from the steam generator and such that the vessel receives the steam condensate from the steam consuming device.
  • one or more heat sources e.g., waste heat source
  • the steam generator may be located in separate locations.
  • additional low-pressure steam may be provided to the steam consuming device by a conventional steam production unit or other steam source (e.g. steam turbine exhaust).
  • a plant may therefore comprise a steam generator and a steam consuming device that are coupled together in a closed cycle configuration such that the steam generator is able to produce and deliver steam at a pressure that is substantially equal to the condensing pressure of the steam in the steam consuming device.
  • the closed cycle further includes a vessel that can receive the steam from the steam generator and that can receive the steam condensate from the steam consuming device.
  • such plants will have at least one or two distinct heat sources (e.g., waste heat, heat transfer fluid, recuperator, etc.) that provide heat to convert the steam condensate into (typically low-pressure) steam having a pressure of equal or less than 50 psia.
  • the inventor also contemplates a method of operating a steam consuming device in which steam is formed in and delivered from a steam generator at a pressure that is substantially equal to a condensing pressure of the steam in the steam consuming device.
  • the step of forming the steam in the steam generator is performed using a heat transfer fluid and/or waste heat source.
  • the steam consuming device and the steam generator are coupled together by a vessel such that the vessel can receive the steam from the steam generator and such that the vessel can receive the steam condensate from the steam consuming device without substantial change in pressure (e.g., compression in a compressor or expansion in an expansion device).
  • additional steam can be delivered from a second steam generator (typically a conventional steam generator or steam turbine exhaust) to the steam consuming device at a suitable pressure.
  • a second steam generator typically a conventional steam generator or steam turbine exhaust
  • excess steam beyond what is required at the steam consuming device can be generated and exported from the system for use in a separate steam consuming device.
  • the steam consuming device is a steam reboiler of a solvent regenerator, and the low-pressure steam has a pressure of equal or less than 50 psia.
  • FIG. 1 is an exemplary schematic illustration of one steam production system according to the inventive subject matter, showing a configuration that is self-contained.
  • FIG. 2 is an exemplary schematic illustration of another steam production system according to the inventive subject matter, showing a configuration that uses supplemental steam and optionally uses multiple heat sources.
  • the present invention is directed to devices and methods for steam generation, and especially low-pressure steam generation in which the steam is generated substantially at the pressure required by the steam consuming device. It should be appreciated that by lowering the steam generation/supply pressure to the required steam consumption pressure, the heat recovered in the steam generation process is maximized, thereby rendering the process more efficient. Moreover, contemplated systems and methods also allow waste heat to be used (e.g., for steam in solvent regeneration) from one or more waste heat sources, which further significantly lowers operating cost of a plant.
  • steam is generated at the lowest possible pressure by having the steam generator fluidly connected to the steam consumer (e.g., reboiler).
  • the steam consumer e.g., reboiler
  • steam generator fluidly connected to the steam consumer (e.g., reboiler).
  • the steam generator e.g., reboiler
  • Such low-pressure steam generation can be achieved by integrating the reboiler condensate drum with the steam drum into the same vessel. Consequently, the steam generator pressure will then ride on the reboiler pressure.
  • Such configurations and methods can advantageously be implemented in plants where the so generated steam is the only heat source or used as a supplemental heat source.
  • contemplated plants will therefore include a steam generator that is fluidly coupled to a steam consuming device, wherein the steam generator produces steam at a pressure that is substantially equal to the condensing pressure of the steam in the steam consuming device.
  • a steam generator that is fluidly coupled to a steam consuming device, wherein the steam generator produces steam at a pressure that is substantially equal to the condensing pressure of the steam in the steam consuming device.
  • one or more heat sources are thermally coupled to the steam generator and configured to provide heat sufficient for converting the steam condensate into the steam.
  • a plant is contemplated that includes a steam generator and a steam consuming device coupled together in a closed cycle configuration such that the steam generator is able to produce and deliver steam at a pressure that is substantially equal to the condensing pressure of the steam in the steam consuming device.
  • FIG. 1 One exemplary configuration is schematically depicted in FIG. 1 where the steam generation unit 100 has a reboiler 110 of a solvent regenerator column as steam consuming device.
  • Steam generator 120 is thermally coupled to heat sources 140 / 142 , respectively, most typically via heat transfer fluid circuit 144 . While it should be appreciated that any heat transfer fluid is deemed suitable for use herein so long as the heat transfer fluid provides sufficient heat for steam generation, especially preferred heat transfer fluids include various flue gases. Further suitable heat transfer fluids include liquid heat transfer media, and even steam.
  • Steam condensate is provided via steam condensate line 126 to the steam generator where at least a portion of the condensate is vaporized, and the steam formed in the steam generator along with the remaining condensate is delivered via steam line 124 .
  • stream 124 will be a two phase stream, typically with a mass vapor fraction of 0.1 to 0.3.
  • Steam 134 is separated from the remaining condensate in vessel 130 that is configured as integrated steam/condensate drum.
  • Steam 134 is then delivered to the reboiler via steam delivery line 124 ′ (substantially completely vapor) and the condensate formed in the reboiler is routed back to the vessel via steam condensate delivery line 126 ′ (substantially completely liquid) where it is stored as condensate 136 .
  • Condensate pump 122 pumps the condensate to the steam generator to so close the steam/condensate closed cycle.
  • the steam/condensate loop could be closed without the pump via natural convection by properly elevating and positioning the steam/condensate drum 130 and steam generator 120 .
  • Line 127 can be used to remove condensate as a blowdown stream for composition control and boiler feed water is provided to the vessel for make-up via level control unit 133 .
  • the steam pressure is preferably controlled via pressure control unit 138 that in the example of FIG. 1 determines the flow of the heat transfer fluid through bypass 145 (i.e. heat input at steam generator 120 ).
  • supplemental steam heat is provided to a plant as exemplarily and schematically shown in the steam generation unit 200 of FIG. 2 .
  • a reboiler 210 of a solvent regenerator column as steam consuming device.
  • Steam generator 220 is thermally coupled to heat source 240 via a heat transfer fluid circuit 244 .
  • Additional steam generators and/or heat sources may be implemented via additional steam line 224 ′′′ (carrying typically between 10-30% vapor in a two-phase stream) and additional steam condensate line 226 ′′.
  • the steam formed in the steam generator(s) is delivered via steam line 224 (carrying typically between 10-30% vapor in a two-phase stream), which contains the steam and remaining condensate, and steam condensate is provided to the steam generator(s) via steam condensate line 226 .
  • Steam 234 is separated from the remaining condensate in vessel 230 that is configured as integrated steam/condensate drum. Steam 234 is then delivered to the reboiler 210 via steam delivery line 224 ′ (substantially completely vapor) and mixed with main steam delivery line 224 ′′.
  • the condensate formed in the reboiler is routed back to the vessel via steam condensate delivery line 226 ′ (substantially completely liquid) where it is stored as condensate 236 .
  • Condensate pump 222 pumps the condensate to the steam generator(s) to so close the supplemental steam/condensate cycle.
  • the steam/condensate loop could be closed without the pump via natural convection by properly elevating and positioning the steam/condensate drum 230 and steam generator 220 .
  • Line 227 is then used to route steam condensate back to the main steam generator (not shown) and is typically controlled by level control unit 233 . Further heat sources, steam generators, regulation of levels and pressures can be achieved as schematically illustrated in FIG. 2 .
  • the steam from the steam generator provides the heat to the reboiler, and that the reboiler steam pressure is indirectly manipulated.
  • the pressure is regulated by adjusting the “make-up” steam and/or by adjusting the heat input at the steam generator such that the heat input required by the process is met at the reboiler. Therefore, as the required pressure rises or falls with the generation pressure, heat recovery is always maximized.
  • Still further contemplated configurations include those in which multiple heat sources are manifolded together (e.g., where multiple boilers all ride on the reboiler condensing pressure) or where excess steam is generated, those in which steam is exported to other steam consuming devices.
  • contemplated systems and methods may be modified in various manners without departing from the inventive concept presented herein.
  • contemplated systems and methods employ a single integrated vessel that is fluidly coupled to the steam generator and the steam consuming device such that the vessel is able to receive the steam from the steam generator and receive the steam condensate from the steam consuming device
  • the vessel may be separated into two distinct but fluidly connected vessels that operate at substantially the same (e.g., with a deviation less than 10% abs.) pressure.
  • steam may be collected in one or more vessels while condensate may be collected in yet further vessels.
  • heat sources are waste heat sources
  • numerous other heat sources are also deemed suitable and include reactor effluent heat (e.g., from catalytic cracking or hydrogenation, reforming, partial oxygenation, Claus furnace, etc.) and combustion heat. Therefore, and depending on the nature and location of the heat source(s), multiple heat sources may be employed in the steam generation according to the inventive subject matter, or the same heat source may provide heat at multiple process points.
  • multiple and distinct heat sources may be arranged in series to heat a heat transfer fluid or the condensate/make-up boiler feed water to a point sufficient for steam generation at the desired pressure. Consequently, it is especially preferred that the heat source directly provides the heat to the steam generator (e.g., using turbine exhaust).
  • the heat transfer medium may also be a fluid or steam and so deliver the heat to the steam generator.
  • the heat source(s) and the steam generator may be located in separate locations, and even more advantageously, that the steam generator and the steam consuming device can be physically separated.
  • the pressure of the steam may vary considerably. However, it is generally preferred that the steam has a pressure of less than 500 psia, more typically less than 250 psia, even more typically less than 100 psia, and most typically less than 50 psia.
  • contemplated methods include also a method of operating a steam consuming device (e.g., steam reboiler of a solvent regenerator) in which in one step steam is formed in and delivered from a steam generator at a pressure that is substantially equal (typically less than 20% deviation, more typically less than 10%, and most typically less than 5% deviation) to a condensing pressure of the steam in the steam consuming device.
  • a steam consuming device e.g., steam reboiler of a solvent regenerator
  • a pressure that is substantially equal typically less than 20% deviation, more typically less than 10%, and most typically less than 5% deviation
  • deviations in pressure between the steam generator and the steam consuming device will typically be such that the difference compensates for line loss pressure drops. Therefore, larger differences are suitable at larger distances between the steam generator and the steam consuming device.
  • the steam is formed in the steam generator using waste heat or other available heat, often at a location other than the location of the steam generator.
  • waste heat may be used to form steam from a steam condensate.
  • the steam consuming device and the steam generator are fluidly coupled together by a vessel such that the vessel is able to (a) receive the steam from the steam generator and (b) receive the steam condensate from the steam consuming device.
  • a vessel such that the vessel is able to (a) receive the steam from the steam generator and (b) receive the steam condensate from the steam consuming device.
  • multiple separate vessels may be used that are coupled together such that one or more vessels collect steam condensate while others collect steam, wherein at least two of these vessels are coupled together such that they operate at substantially the same pressure.
  • contemplated configurations and methods may be implemented as stand-alone steam providers or in a configuration where supplemental steam is delivered to a steam consuming device next to utility steam at the pressure needed at the steam consuming device.
  • contemplated system and methods provide multiple advantages over currently known configurations and methods.
  • the heat source for steam generation and the steam consuming device e.g., the reboiler
  • the steam consuming device can be physically separated and therefore avoid complex ducting and/or piping arrangements.
  • hydraulic requirements of the reboiler system or other steam consuming device can be preserved.
  • the skin temperature of the reboiler tubes or other heat transfer surface is not affected by the temperature of the heat source, thereby avoiding problems associated with excessive temperatures in the reboiler system, such as thermal degradation of the process fluid.
  • a yet further advantage of contemplated configurations and methods is that multiple heat sources can be utilized to generate a combined steam flow, thereby keeping the reboiler configuration or other steam consuming devices simple.
  • contemplated systems and methods are preferably used in a reboiler of a solvent regenerator
  • the configurations and methods may be employed in numerous alternative uses, and indeed in any situation where low-pressure steam heating is required.
  • contemplated systems and methods are implemented in plants that have significant levels of low level waste heat (e.g., in a power plant, hydrotreating and/or hydrocracking plant, sulfur recovery plant, a syngas producing plant, a Fischer-Tropsch plant, etc.).
  • contemplated configurations and methods are implemented in a flue gas treatment system, and especially in a retrofit project that has excess waste heat.

Landscapes

  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)
  • Control Of Steam Boilers And Waste-Gas Boilers (AREA)
  • Treating Waste Gases (AREA)
US13/390,024 2009-08-11 2009-08-11 Configurations and methods of generating low-pressure steam Active 2030-12-18 US9320985B2 (en)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/US2009/053370 WO2011019335A1 (en) 2009-08-11 2009-08-11 Configurations and methods of generating low-pressure steam

Publications (2)

Publication Number Publication Date
US20120204817A1 US20120204817A1 (en) 2012-08-16
US9320985B2 true US9320985B2 (en) 2016-04-26

Family

ID=43586326

Family Applications (1)

Application Number Title Priority Date Filing Date
US13/390,024 Active 2030-12-18 US9320985B2 (en) 2009-08-11 2009-08-11 Configurations and methods of generating low-pressure steam

Country Status (11)

Country Link
US (1) US9320985B2 (ja)
EP (1) EP2464435B1 (ja)
JP (1) JP5738293B2 (ja)
CN (1) CN102625726B (ja)
AU (1) AU2009351096B2 (ja)
CA (1) CA2770596C (ja)
EA (1) EA201270250A1 (ja)
IN (1) IN2012DN01217A (ja)
MX (1) MX2012001808A (ja)
WO (1) WO2011019335A1 (ja)
ZA (1) ZA201201538B (ja)

Families Citing this family (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2984177B1 (fr) * 2011-12-20 2014-07-04 IFP Energies Nouvelles Procede de craquage catalytique associe a une unite de traitement aux amines avec bilan co2 ameliore
US9108123B2 (en) 2012-07-26 2015-08-18 Fluor Technologies Corporation Steam efficiency with non depletive condensing and adiabatic solvent heating
US9314732B2 (en) 2013-01-09 2016-04-19 Fluor Technologies Corporation Systems and methods for reducing the energy requirements of a carbon dioxide capture plant
US9803513B2 (en) 2015-08-24 2017-10-31 Saudi Arabian Oil Company Power generation from waste heat in integrated aromatics, crude distillation, and naphtha block facilities
US9803511B2 (en) 2015-08-24 2017-10-31 Saudi Arabian Oil Company Power generation using independent dual organic rankine cycles from waste heat systems in diesel hydrotreating-hydrocracking and atmospheric distillation-naphtha hydrotreating-aromatics facilities
US9803506B2 (en) 2015-08-24 2017-10-31 Saudi Arabian Oil Company Power generation from waste heat in integrated crude oil hydrocracking and aromatics facilities
US9803508B2 (en) 2015-08-24 2017-10-31 Saudi Arabian Oil Company Power generation from waste heat in integrated crude oil diesel hydrotreating and aromatics facilities
US9803505B2 (en) 2015-08-24 2017-10-31 Saudi Arabian Oil Company Power generation from waste heat in integrated aromatics and naphtha block facilities
US9803509B2 (en) 2015-08-24 2017-10-31 Saudi Arabian Oil Company Power generation from waste heat in integrated crude oil refining and aromatics facilities
US9803507B2 (en) * 2015-08-24 2017-10-31 Saudi Arabian Oil Company Power generation using independent dual organic Rankine cycles from waste heat systems in diesel hydrotreating-hydrocracking and continuous-catalytic-cracking-aromatics facilities
US9827602B2 (en) 2015-09-28 2017-11-28 Tesla, Inc. Closed-loop thermal servicing of solvent-refining columns
CN107893987A (zh) * 2017-12-28 2018-04-10 西安富凯能源科技有限责任公司 自然循环锅炉水动力的高效利用系统
CN114367118A (zh) * 2021-12-22 2022-04-19 泰兴金江化学工业有限公司 一种乙酸乙酯生产用锆材再沸器

Citations (21)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3213833A (en) * 1960-12-30 1965-10-26 Westinghouse Electric Corp Unitized vapor generation system
US3442613A (en) 1965-10-22 1969-05-06 Braun & Co C F Hydrocarbon reforming for production of a synthesis gas from which ammonia can be prepared
US3666828A (en) 1970-09-14 1972-05-30 Phillips Petroleum Co Condensate purification and recovery for use as dilution steam to pyrolysis furnace
EP0113530A2 (en) 1982-12-23 1984-07-18 Air Products And Chemicals, Inc. Process and plant for removing methane and argon from crude ammonia synthesis gas
US4555310A (en) 1978-08-30 1985-11-26 Phillips Petroleum Company Method of utilizing energy of high pressure condensate
US4829938A (en) * 1987-09-28 1989-05-16 Mitsubishi Jukogyo Kabushiki Kaisha Exhaust boiler
US4930316A (en) * 1988-07-11 1990-06-05 Magma Power Company Geothermal plant noncondensable gas removal and heat recovery system and method
US5330618A (en) * 1992-12-10 1994-07-19 University Of Chicago Process for separating dissolved solids from a liquid using an anti-solvent and multiple effect evaporators
US20020102200A1 (en) 2000-04-10 2002-08-01 Jungerhans Robert Rudolf Josef Purification of gases, in synthesis gas production process
WO2003002459A1 (en) 2001-06-28 2003-01-09 Fluor Corporation Improved ammonia plant configurations and methods
JP2003222301A (ja) 2002-01-31 2003-08-08 Hitachi Ltd 産業用プロセス蒸気発生設備の運転制御方法およびシステム
JP2003343212A (ja) 2002-05-24 2003-12-03 Toyota Motor Corp 高温蒸気タービン発電装置
US20040059070A1 (en) 2002-09-19 2004-03-25 Whitte William M. Process and apparatus for controlling molecular weight distribution and short chain branching for olefin polymers
WO2007075466A2 (en) 2005-12-19 2007-07-05 Fluor Technologies Corporation Integrated compressor/stripper configurations and methods
WO2007113308A1 (en) 2006-04-03 2007-10-11 Total Petrochemicals Research Feluy Process for improving the polymerization of ethylene and one or more optional co-monomer(s) in a polymerization loop reactor
US20080276617A1 (en) * 2005-03-30 2008-11-13 John Mak Configurations and Methods For Thermal Integration of Lng Regasification and Power Plants
US20100126433A1 (en) 2008-11-21 2010-05-27 Hitachi, Ltd. Liquid level control system
US8091361B1 (en) * 2007-11-05 2012-01-10 Exergetic Systems, Llc Method and apparatus for controlling the final feedwater temperature of a regenerative Rankine cycle using an exergetic heater system
US8118895B1 (en) * 2007-03-30 2012-02-21 Bechtel Power Corporation Method and apparatus for refueling existing natural gas combined cycle plant as a non-integrated gasification combined cycle plant
US20120055158A1 (en) * 2009-04-30 2012-03-08 Rwe Power Aktiengesellschaft Method for operating a steam turbine power plant and device for producing steam from lignite
US20140026755A1 (en) * 2012-07-26 2014-01-30 Fluor Technologies Corporation Steam efficiency with non depletive condensing and adiabatic solvent heating

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2785272A (en) * 1955-04-25 1957-03-12 Hal H Baly Steam generator
DE2734031C2 (de) * 1977-07-28 1982-07-29 Ferdinand Lentjes, Dampfkessel- und Maschinenbau, 4000 Düsseldorf Mobiler Naßdampf-Zwangsdurchlaufdampferzeuger
DE19505608C2 (de) * 1995-02-18 1997-08-14 Kaercher Gmbh & Co Alfred Dampfreinigungsgerät
JP3790297B2 (ja) * 1996-05-24 2006-06-28 三菱重工業株式会社 重質油焚き複合発電設備
EP1537359B1 (en) * 2002-08-26 2012-09-12 Koninklijke Philips Electronics N.V. Electric steaming device

Patent Citations (22)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3213833A (en) * 1960-12-30 1965-10-26 Westinghouse Electric Corp Unitized vapor generation system
US3442613A (en) 1965-10-22 1969-05-06 Braun & Co C F Hydrocarbon reforming for production of a synthesis gas from which ammonia can be prepared
US3666828A (en) 1970-09-14 1972-05-30 Phillips Petroleum Co Condensate purification and recovery for use as dilution steam to pyrolysis furnace
US4555310A (en) 1978-08-30 1985-11-26 Phillips Petroleum Company Method of utilizing energy of high pressure condensate
EP0113530A2 (en) 1982-12-23 1984-07-18 Air Products And Chemicals, Inc. Process and plant for removing methane and argon from crude ammonia synthesis gas
US4829938A (en) * 1987-09-28 1989-05-16 Mitsubishi Jukogyo Kabushiki Kaisha Exhaust boiler
US4930316A (en) * 1988-07-11 1990-06-05 Magma Power Company Geothermal plant noncondensable gas removal and heat recovery system and method
US5330618A (en) * 1992-12-10 1994-07-19 University Of Chicago Process for separating dissolved solids from a liquid using an anti-solvent and multiple effect evaporators
US20020102200A1 (en) 2000-04-10 2002-08-01 Jungerhans Robert Rudolf Josef Purification of gases, in synthesis gas production process
WO2003002459A1 (en) 2001-06-28 2003-01-09 Fluor Corporation Improved ammonia plant configurations and methods
JP2003222301A (ja) 2002-01-31 2003-08-08 Hitachi Ltd 産業用プロセス蒸気発生設備の運転制御方法およびシステム
JP2003343212A (ja) 2002-05-24 2003-12-03 Toyota Motor Corp 高温蒸気タービン発電装置
US20040059070A1 (en) 2002-09-19 2004-03-25 Whitte William M. Process and apparatus for controlling molecular weight distribution and short chain branching for olefin polymers
US20080276617A1 (en) * 2005-03-30 2008-11-13 John Mak Configurations and Methods For Thermal Integration of Lng Regasification and Power Plants
WO2007075466A2 (en) 2005-12-19 2007-07-05 Fluor Technologies Corporation Integrated compressor/stripper configurations and methods
WO2007113308A1 (en) 2006-04-03 2007-10-11 Total Petrochemicals Research Feluy Process for improving the polymerization of ethylene and one or more optional co-monomer(s) in a polymerization loop reactor
US8118895B1 (en) * 2007-03-30 2012-02-21 Bechtel Power Corporation Method and apparatus for refueling existing natural gas combined cycle plant as a non-integrated gasification combined cycle plant
US8091361B1 (en) * 2007-11-05 2012-01-10 Exergetic Systems, Llc Method and apparatus for controlling the final feedwater temperature of a regenerative Rankine cycle using an exergetic heater system
US20100126433A1 (en) 2008-11-21 2010-05-27 Hitachi, Ltd. Liquid level control system
JP2010121916A (ja) 2008-11-21 2010-06-03 Hitachi Ltd 液位制御システム。
US20120055158A1 (en) * 2009-04-30 2012-03-08 Rwe Power Aktiengesellschaft Method for operating a steam turbine power plant and device for producing steam from lignite
US20140026755A1 (en) * 2012-07-26 2014-01-30 Fluor Technologies Corporation Steam efficiency with non depletive condensing and adiabatic solvent heating

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
P.I. Voskresenskiy, "Technique of laboratory works", M1973, pp. 449-450, fig. 380.

Also Published As

Publication number Publication date
AU2009351096A1 (en) 2012-03-01
EA201270250A1 (ru) 2012-07-30
IN2012DN01217A (ja) 2015-04-10
ZA201201538B (en) 2014-10-29
JP5738293B2 (ja) 2015-06-24
EP2464435B1 (en) 2019-11-20
US20120204817A1 (en) 2012-08-16
EP2464435A1 (en) 2012-06-20
CA2770596A1 (en) 2011-02-17
EP2464435A4 (en) 2018-03-21
CN102625726B (zh) 2015-02-18
AU2009351096B2 (en) 2013-10-24
WO2011019335A1 (en) 2011-02-17
JP2013501912A (ja) 2013-01-17
MX2012001808A (es) 2012-04-11
CN102625726A (zh) 2012-08-01
CA2770596C (en) 2015-11-03

Similar Documents

Publication Publication Date Title
US9320985B2 (en) Configurations and methods of generating low-pressure steam
US12065398B2 (en) Use of renewable energy in methanol synthesis
US11939915B2 (en) Raw material fluid treatment plant and raw material fluid treatment method
US20100314878A1 (en) Direct Generation of Steam Motive Flow by Water-Cooled Hydrogen/Oxygen Combustion
US20080034757A1 (en) Method and system integrating solar heat into a regenerative rankine cycle
EP2942497B1 (en) Oxy boiler power plant oxygen feed system heat integration
CN117136255A (zh) 离岸可再生能源发电站
EP3730473A1 (en) Use of renewable energy in methanol synthesis
JP2011231320A5 (ja)
AU2001245857A1 (en) Method and system for generating power
CN101793174B (zh) 降低气化系统中冷却水和动力消耗的系统及其组装方法
CN104279543B (zh) 锅炉系统
WO2001071176A2 (en) Method and system for generating power
JP3652743B2 (ja) ガス化複合発電プラント
CN104040274A (zh) 空气分离、功率生成的集成
US20230058456A1 (en) Power generation system
US20230243279A1 (en) Heat integration
EP4187061A1 (en) Method and apparatus for co-generating electricity in a process plant integrated with a thermal power generator
US8943838B2 (en) Integrated turbomachine plant
KR20230154265A (ko) 증기 분해 방법 및 시스템
RU2287704C1 (ru) Тепловая электрическая станция
JP2001050011A (ja) 石油燃料燃焼コンバインドサイクル発電施設及びその発電施設の運転方法。
CN118434958A (zh) 带有绝热压缩的co2动力循环
JP2001041006A (ja) 石油燃料燃焼コンバインドサイクル発電施設及びその発電施設の運転方法。
JPH0261465A (ja) 燃料改質システム

Legal Events

Date Code Title Description
AS Assignment

Owner name: FLUOR TECHNOLOGIES CORPORATION, CALIFORNIA

Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNOR:SHERFFIUS, JEFFREY;REEL/FRAME:023164/0900

Effective date: 20090824

AS Assignment

Owner name: FLUOR TECHNOLOGIES CORPORATION, CALIFORNIA

Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNOR:SCHERFFIUS, JEFFREY;REEL/FRAME:028122/0854

Effective date: 20120322

STCF Information on status: patent grant

Free format text: PATENTED CASE

MAFP Maintenance fee payment

Free format text: PAYMENT OF MAINTENANCE FEE, 4TH YEAR, LARGE ENTITY (ORIGINAL EVENT CODE: M1551); ENTITY STATUS OF PATENT OWNER: LARGE ENTITY

Year of fee payment: 4

MAFP Maintenance fee payment

Free format text: PAYMENT OF MAINTENANCE FEE, 8TH YEAR, LARGE ENTITY (ORIGINAL EVENT CODE: M1552); ENTITY STATUS OF PATENT OWNER: LARGE ENTITY

Year of fee payment: 8